WO2019060324A2 - Utilisation d'une paroi de séparation supérieure dans une unité d'isomérisation - Google Patents

Utilisation d'une paroi de séparation supérieure dans une unité d'isomérisation Download PDF

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Publication number
WO2019060324A2
WO2019060324A2 PCT/US2018/051584 US2018051584W WO2019060324A2 WO 2019060324 A2 WO2019060324 A2 WO 2019060324A2 US 2018051584 W US2018051584 W US 2018051584W WO 2019060324 A2 WO2019060324 A2 WO 2019060324A2
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WO
WIPO (PCT)
Prior art keywords
dividing wall
wall column
column
stream
overheads
Prior art date
Application number
PCT/US2018/051584
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English (en)
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WO2019060324A3 (fr
Inventor
Manish BHARGAVA
Roomi Kalita
Joseph C. Gentry
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Gtc Technology Us Llc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Gtc Technology Us Llc filed Critical Gtc Technology Us Llc
Priority to MX2020002915A priority Critical patent/MX2020002915A/es
Priority to US16/648,447 priority patent/US11161055B2/en
Priority to ES18857670T priority patent/ES2948682T3/es
Priority to CN201880060580.XA priority patent/CN111107916B/zh
Priority to PL18857670.6T priority patent/PL3664906T3/pl
Priority to KR1020207010864A priority patent/KR102560529B1/ko
Priority to EA202090743A priority patent/EA202090743A1/ru
Priority to EP18857670.6A priority patent/EP3664906B1/fr
Priority to JP2020537451A priority patent/JP7202388B2/ja
Priority to CA3076204A priority patent/CA3076204C/fr
Priority to AU2018335261A priority patent/AU2018335261B2/en
Publication of WO2019060324A2 publication Critical patent/WO2019060324A2/fr
Publication of WO2019060324A3 publication Critical patent/WO2019060324A3/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/141—Fractional distillation or use of a fractionation or rectification column where at least one distillation column contains at least one dividing wall
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/009—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in combination with chemical reactions
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/06—Flash distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
    • B01D3/148—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step in combination with at least one evaporator
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
    • B01D3/322—Reboiler specifications
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
    • B01D5/006—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with evaporation or distillation
    • B01D5/0063—Reflux condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
    • B01J8/0476—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more otherwise shaped beds
    • B01J8/0484—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more otherwise shaped beds the beds being placed next to each other
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
    • B01J8/0476—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more otherwise shaped beds
    • B01J8/0488—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more otherwise shaped beds the beds being placed in separate reactors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0492—Feeding reactive fluids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
    • B01J8/065—Feeding reactive fluids
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
    • C07C5/27—Rearrangement of carbon atoms in the hydrocarbon skeleton
    • C07C5/2702—Catalytic processes not covered by C07C5/2732 - C07C5/31; Catalytic processes covered by both C07C5/2732 and C07C5/277 simultaneously
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/005—Processes comprising at least two steps in series
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/04—Purification; Separation; Use of additives by distillation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/11—Purification; Separation; Use of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including at least two different refining steps in the absence of hydrogen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G7/00—Distillation of hydrocarbon oils
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G7/00—Distillation of hydrocarbon oils
    • C10G7/02—Stabilising gasoline by removing gases by fractioning
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/02—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles
    • B01J2208/023—Details
    • B01J2208/024—Particulate material
    • B01J2208/025—Two or more types of catalyst
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1044—Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C

Definitions

  • the claimed invention relates generally to top dividing wall columns and more particularly, but not by way of limitation, to an improved isomerization unit that reduces cost and increases efficiency.
  • a naphtha hydrotreating (NHT) and isomerization unit 100 is comprised of multiple conventional distillation columns as shown in FIG.1.
  • a feed stream from an NHT reactor is sent to a first stabilizer column 102.
  • the first stabilizer column 102 removes non-condensable components from the feed stream as off-gas.
  • a stabilized bottoms product stream is fed from the first stabilizer column 102 to a naphtha splitter column 104.
  • the naphtha splitter column 104 separates the stabilized bottom product into a light naphtha overhead stream and heavy naphtha bottoms stream.
  • the light naphtha overhead stream is comprised mainly of C5 - C 6 components.
  • the light naphtha overhead stream is fed to a deisopentanizer column 106, which concentrates 1-C5 as an overhead stream of the deisopentanizer column 106.
  • the remaining C5-C6 components are obtained as a bottoms stream of the deisopentanizer column 106 and are fed to an isomerization reactor 108 for octane upgrading.
  • unstable isomerate from the isomerization reactor 108 is further processed in a second stabilizer column 110.
  • a C5 rich stream from the depentanizer column 112 is recycled back to the deisopentanizer column 106 upstream to remove 1-C5 product.
  • the bottoms product stream from the depentanizer column 112 is fed to a deisohexanizer column 114.
  • a C 6 isomerate product stream is removed from the deisohexanizer column 114 as an overhead stream and a heavy isomerate product stream (mainly C 7+ cut) is removed from the deisohexanizer column 114 as bottoms stream.
  • An n-C 6 rich cut is removed as a side cut from the deisohexanizer column 114 and is recycled to the isomerization reactor.
  • the prior art system 100 of FIG. 1 possesses several disadvantages.
  • the first and second stabilizer columns 102, 110 in the prior art system 100 operate at relatively high pressures (-100 psig and -160 psig respectively in this case). Due to the partial condensation used in conventional stabilizers, liquid losses to off gas are high.
  • the naphtha splitter column 104 also operates at a high pressure (-75 psig). Consequently, the column reboilers operate on moderately expensive medium pressure (MP) steams.
  • MP medium pressure
  • Dividing wall column (DWC) technology enables improvements to the efficiency and cost of traditional isomerization process schemes.
  • An embodiment of the invention is directed to a process wherein isomerization is used to obtain high octane C5 and C 6 components for gasoline blending.
  • An embodiment of the invention includes an application wherein a multi-column isomerization configuration is replaced with lesser number of distillation columns utilizing a DWC concept. Due to a combination of lower operating column pressures and improved heat integration within the system, DWC configurations consume significantly less energy and reduce the cost of heating.
  • An embodiment of the invention encompasses hydro-treating reactor stabilizer columns, wherein a first stabilizer column and a downstream naphtha splitter column are combined into a single top dividing wall column (e.g., See FIGS. 2 and 3). Such an arrangement produces the similar number of products, while reducing the number of columns from two to one.
  • the new hybrid column operates at the same pressure as a conventional stabilizer.
  • a DWC includes a dividing wall positioned in a top section of the DWC to form two top halves, wherein the two top halves act as independent columns.
  • the first stabilizer column and naphtha splitter column of the prior art system of FIG.l are combined into a top dividing wall column (e.g., see FIGS. 2 and 3).
  • the side of the DWC where the stream enters operates as an absorber.
  • a lean naphtha stream is used as the absorption medium. This lean naphtha stream can be obtained either from a heavier bottoms of the DWC column or from another nearby column within the same complex.
  • the other side of the DWC operates like a typical distillation column.
  • an embodiment of the invention encompasses such columns, wherein both distillation and absorption are carried out within the same column.
  • the depentanizer and deisohexanizer columns of the prior art system of FIG.l can also be combined into a top DWC (e.g., see FIGS. 2 and 4).
  • a top portion of the DWC behaves as two separation zones.
  • One side acts as a depentanizer to remove C5 components, while the other side operates as a deisohexanizer column to recover light (mainly C 6 isomerate) and heavy isomerate (C 7 and heavier) products.
  • the isomerization stabilizer is operated at a lower pressure than the prior art system of FIG. 1.
  • the pressure may be around 75 psig, as compared to around 160 psig for the second stabilizer column of the prior art system of FIG. 1.
  • the operating pressure has been selected such that, compared to the prior art system of FIG. 1, the second stabilizer column operates with lower temperature heating utility (low pressure steam in this case). Additionally, some reboiling duty to the second stabilizer column is obtained by heat integration with reactor effluent bottoms from the isomerization reactor.
  • the DWC comprising the first stabilizer column and the naphtha splitter column is operated at a high pressure (-100 psig) as well.
  • This arrangement compensates for the lower operating pressure of the downstream second stabilizer column.
  • the valuable C5 components lost in the latter system is captured in the upstream DWC column by means of absorption using a lean naphtha stream.
  • this arrangement facilitates heat integration with the deisopentanizer column.
  • a packed flash drum is used wherein off-gas from the second stabilizer is stripped using a part of the heavy naphtha bottoms from DWC column that combines the first stabilizer column and the naphtha splitter column.
  • the residual lean naphtha stream is obtained as the liquid product from the drum and used as the absorption medium in the configuration.
  • the system utilizes a combination of low pressure (LP) and medium (MP) steam by applying DWC technology to the configuration provides significant reduction in utility costs as compared to the prior art system of FIG.1.
  • LP low pressure
  • MP medium
  • FIG. 1 represents a prior art system of a combined naphtha hydrotreating and isomerization unit
  • FIG. 2 represents a process scheme in accordance with an embodiment of the invention for using DWC technology in a naphtha hydrotreating and isomerization unit;
  • FIG. 3 represents a process scheme in accordance with an embodiment of the invention for a top DWC stabilizer/naphtha splitter design
  • FIG. 4 represents a process scheme in accordance with an embodiment of the invention for a top DWC depentanizer/deisohexanizer design.
  • Embodiments of the invention are directed to an isomerization process wherein individual columns are replaced and/or combined together using DWC technology with the objective of minimizing utility consumption.
  • Scheme 200 includes a first divided wall column (DWC) 210 and a second DWC 240.
  • First DWC 210 includes a top dividing wall 211 that divides a top portion 212 of first DWC 210 into a first side 213 and a second side 214.
  • first side 213 is configured to operate as a stabilizer column and second side 214 is configured to operate as a naphtha splitter column.
  • first side 213 includes a first overheads section 215 and second side 214 includes a second overheads section 216.
  • a first condenser 217 is coupled to first overheads section 215 and is configured to condense overheads received therefrom. Reflux from first condenser 217 can be fed back to first overheads section 215.
  • a second condenser 218 is coupled to second overheads section 216 and is configured to condense overheads received therefrom. Reflux from second condenser 218 can be fed back to second overheads section 216.
  • a bottoms reboiler 219 is coupled to first DWC 210 and is configured to receive a bottoms stream from first DWC 210 and to return a heated stream back to a bottoms section 220 of first DWC 210.
  • Second DWC 240 includes a top dividing wall 241 that divides a top portion 242 of second DWC 240 into a first side 243 and a second side 244.
  • first side 243 is configured to operate as a depentanizer column and second side 244 is configured to operate as a deisohexanizer column.
  • first side 243 includes a first overheads section 245 and second side 244 includes a second overheads section 246.
  • a first condenser 247 is coupled to first overheads section 245 and is configured to condense overheads received therefrom. Reflux from first condenser 247 can be fed back to first overheads section 245.
  • a second condenser 248 is coupled to second overheads section 246 and is configured to condense overheads received therefrom. Reflux from second condenser 248 can be fed back to second overheads section 246.
  • a bottoms reboiler 249 is coupled to second DWC 240 and is configured to receive a bottoms stream from second DWC 240 and to return a heated stream back to a bottoms section 250 of second DWC 240.
  • An exemplary process flow for scheme 200 begins by feeding a stream 230 to first side 213 of first DWC 210.
  • first side 213 is a stabilizer and second side 214 is a naphtha splitter.
  • stream 230 is sourced from a naphtha hydrotreating reactor.
  • First side 213 removes non-condensable components from stream 230 as off-gas stream 231.
  • a stabilized bottoms product descends first side 213 and enters second side 214.
  • Second side 214 separates the stabilized bottom product from first side 213 into a light naphtha overhead stream 232 and heavy naphtha bottoms stream 233.
  • the light naphtha overhead stream 232 is comprised mainly of C5 - C 6 components.
  • Light naphtha overhead stream 232 is fed to a deisopentanizer column 251, which concentrates 1-C5 as an overhead stream 234.
  • the remaining C5-C6 components are obtained as a bottoms stream 235 of deisopentanizer column 251 and are fed to an isomerization reactor 252 for octane upgrading via isomerization reactions.
  • a stream 236 containing unstable isomerate from isomerization reactor 252 is further processed in a stabilizer column 254.
  • first side 243 is a depentanizer and second side 244 is a deisohexanizer.
  • An overheads stream 261 that is rich in C5 is recycled from the first overheads section 245 of second DWC 240 to deisopentanizer column 251 upstream to remove 1-C5 product.
  • a bottoms product stream descends first side 243 and enters second side 244.
  • a C 6 isomerate product stream 262 is removed from second DWC 240 as an overhead stream and a heavy isomerate product stream 263 (mainly C 7+ cut) is removed from second DWC 240 as bottoms stream.
  • An n-C 6 rich stream 264 is removed as a side cut from second DWC 240 and is recycled to the isomerization reactor 252.
  • FIG. 3 is a side-by-side comparison of columns 102 and 104 of FIG. 1 with first DWC 210 of FIG. 2.
  • Top dividing wall 211 segregates the top portion 212 of first DWC 210 into first side 213 and second side 214, namely the pre-fractionation side and the product side for reference.
  • the process scheme is designed to remove the non-condensable as off-gas stream 231. Additionally, the scheme concentrates middle boiling components (C5- C 7 ) as light naphtha overhead stream 232 on the other side, while the heaviest boiling components (heavy naphtha) are recovered at the bottom of the column as heavy naphtha bottoms stream 233.
  • first condenser 217 on the absorption side is a partial water-cooled condenser
  • second condenser 218 on the distillation side is a total condenser using an air-cooled exchanger.
  • DWC 212 operates at a high operating pressure of 100 psig and utilizes MP steam as the heating medium in bottoms reboiler 219 (e.g., a thermosiphon reboiler).
  • the high temperature of the column allows heat integration with the downstream deisopentanizer column 251 that operates at a significantly lower pressure.
  • Deisopentanizer column 251 is a conventional distillation column which removes an isopentane concentrated stream at the top (overhead stream 234).
  • a reboiler of deisopentanizer column 251 utilizes LP steam, while another reboiler is heat integrated with the hot overhead C5-C7 vapors from the upstream DWC 212.
  • FIG. 4 is a side-by-side comparison of columns 112 and 114 of FIG. 1 with second DWC 240 of FIG. 2.
  • Second DWC 240 separates four product streams: a C 5 recycle stream 261, C 6 isomerate stream 262, and C7+ stream 263 along with a n-C 6 recycle stream 264.
  • Two total condensers 247, 248 are available on both sides of top dividing wall 241.
  • condensers 247, 248 are air-cooled exchangers.
  • Bottoms reboiler 249 at the bottom of second DWC 240 operates on LP steam.
  • column overhead pressures are maintained via a pressure controller on the overhead vapor product line.
  • the pre-fractionation side has reflux coming from the overhead condenser.
  • Table 1 below highlights energy and cost savings of scheme 200 versus prior art system 100.

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  • Chemical & Material Sciences (AREA)
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  • Chemical Kinetics & Catalysis (AREA)
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  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
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  • Water Supply & Treatment (AREA)
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  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Acyclic And Carbocyclic Compounds In Medicinal Compositions (AREA)
  • Apparatus Associated With Microorganisms And Enzymes (AREA)
  • Sewage (AREA)
  • Cultivation Receptacles Or Flower-Pots, Or Pots For Seedlings (AREA)

Abstract

L'invention concerne un schéma combiné d'hydrotraitement de naphta (NHT) et d'isomérisation, qui comprend des colonnes de paroi séparatrices (DWC) qui remplacent de multiples colonnes de distillation et permettent une intégration de chaleur optimisée dans le système. La conception de l'invention permet des réductions des coûts de capital et d'énergie par rapport aux schémas classiques.
PCT/US2018/051584 2017-09-19 2018-09-18 Utilisation d'une paroi de séparation supérieure dans une unité d'isomérisation WO2019060324A2 (fr)

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MX2020002915A MX2020002915A (es) 2017-09-19 2018-09-18 Uso de pared divisoria superior en unidad de isomerizacion.
US16/648,447 US11161055B2 (en) 2017-09-19 2018-09-18 Use of top dividing wall in isomerization unit
ES18857670T ES2948682T3 (es) 2017-09-19 2018-09-18 Uso de una pared divisoria superior en unidad de isomerización
CN201880060580.XA CN111107916B (zh) 2017-09-19 2018-09-18 在异构化单元中使用顶部分隔壁
PL18857670.6T PL3664906T3 (pl) 2017-09-19 2018-09-18 Zastosowanie górnej pionowej przegrody w jednostce izomeryzacji
KR1020207010864A KR102560529B1 (ko) 2017-09-19 2018-09-18 이성질화 유닛에서 상부 분리벽의 사용
EA202090743A EA202090743A1 (ru) 2017-09-19 2018-09-18 Использование верхней разделительной перегородки в установке изомеризации
EP18857670.6A EP3664906B1 (fr) 2017-09-19 2018-09-18 Utilisation d'une paroi de séparation supérieure dans une unité d'isomérisation
JP2020537451A JP7202388B2 (ja) 2017-09-19 2018-09-18 異性化ユニットにおける上部分割壁の使用
CA3076204A CA3076204C (fr) 2017-09-19 2018-09-18 Utilisation d'une paroi de separation superieure dans une unite d'isomerisation
AU2018335261A AU2018335261B2 (en) 2017-09-19 2018-09-18 Use of top dividing wall in isomerization unit

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US201762560569P 2017-09-19 2017-09-19
US62/560,569 2017-09-19

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WO2021233801A1 (fr) * 2020-05-20 2021-11-25 Sulzer Management Ag Intégration de chaleur par l'intermédiaire d'une pompe à chaleur sur une colonne de paroi de séparation inférieure

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EP4234660A1 (fr) * 2022-02-25 2023-08-30 Sulzer Management AG Procédé et installation de production de n-hexane et d'isomérat efficace en énergie et ayant un indice d'octane élevé
WO2023161267A1 (fr) * 2022-02-25 2023-08-31 Sulzer Management Ag Procédé et installation de production énergétique efficace de n-hexane et d'isomérat à indice d'octane élevé

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HUE062291T2 (hu) 2023-10-28
EP3664906C0 (fr) 2023-06-07
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EP3664906A2 (fr) 2020-06-17
KR102560529B1 (ko) 2023-07-27
CN111107916A (zh) 2020-05-05
CA3076204A1 (fr) 2019-03-28
EP3664906B1 (fr) 2023-06-07
CA3076204C (fr) 2023-09-19
US20200223771A1 (en) 2020-07-16
US10653974B2 (en) 2020-05-19
US11161055B2 (en) 2021-11-02
JP2020534154A (ja) 2020-11-26
PL3664906T3 (pl) 2023-12-04
WO2019060324A3 (fr) 2019-05-02
EP3664906A4 (fr) 2021-03-24
US20190083898A1 (en) 2019-03-21
ES2948682T3 (es) 2023-09-15
EA202090743A1 (ru) 2020-06-19
KR20200055044A (ko) 2020-05-20
JP7202388B2 (ja) 2023-01-11
CN111107916B (zh) 2022-02-18
MX2020002915A (es) 2020-07-22

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